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Environ. Eng. Res. 2022
Research Article https://doi.org/10.4491/eer.2020.683
pISSN 1226-1025 eISSN 2005-968X
In Press, Uncorrected Proof
Investigation of the thermodynamic performance of an
existing steam power plant via energy and exergy analyses
to restrain the environmental repercussions: A simulation
study
Muhammad Haris Hamayun1, Murid Hussain
1†, Iqrash Shafiq
1, Ashfaq Ahmed
1,2†, Young-Kwon Park
2†
1Department of Chemical Engineering, COMSATS University Islamabad, Lahore Campus 54000, Lahore, Pakistan 2School of Environmental Engineering, University of Seoul, Seoul, 02504, Republic of Korea
Abstract
Exergy analysis is an important tool to identify the improvements in various industrial processes. In this study, the
existing steam power plant is examined based on energy and exergy analyses. The steam network in the power plant
is comprised of two sections, one of them is used for paddy drying, while other portion is used to operate the
turbine for in-house electricity production. Mass, energy, and exergy balances are applied to individual equipment
of the plant. The power plant is modeled and simulated using Aspen HYSYS® V10. The calculated thermodynamic
values are used for in-depth analysis of the power plant. Case-studies are included in this study to show the effect of
various operational parameters on the process efficiency. The analysis shows that the boiler is the major source of
exergy destruction, because of the incomplete combustion process, and inappropriate insulations. The remedial
actions are also suggested in the study.
Keywords: Exergy analysis, Exergy efficiency, Exergy destruction, Case study, Process Simulation
This is an Open Access article distributed under the terms
of the Creative Commons Attribution Non-Commercial Li-
cense (http://creativecommons.org/licenses/by-nc/3.0/)
which permits unrestricted non-commercial use, distribution, and repro-
duction in any medium, provided the original work is properly cited.
Received December 10, 2020 Accepted January 06, 2021
† Corresponding Author
E-mail: [email protected], [email protected]
Tel: +92-42-99205226, +82 10 4325 6899, +82-2-6490-2870
Fax: +82-2-6490-2859
ORCID: 0000-0002-2271-0869
Copyright © 2020 Korean Society of Environmental Engineers http://eeer.org
2
1. Introduction 1
For the economic growth of a country, power generation companies play a vital role. A 2
universally available form of energy is electrical energy, which can be converted into all other 3
forms of energy and its demand has increased with time [1]. Powerhouses are installed in a 4
considerable number in Pakistan for electrical energy generation, 75% of which are using coal as 5
fuel. In these power plants, energy optimization is an important aspect regarding the decrease in 6
the fuel consumption rate [2]. Energy consumption is an important parameter to reflect a 7
country`s development stages and its communities living standards [3]. Power plant efficiency is 8
a critical and important parameter regarding the decrease in fossil fuel consumption rate as it is a 9
primary energy source for power generation, industry, and transportation [4]. However, in many 10
countries, from power generation cycles, steam power cycles are now being rejected because of 11
reduced efficiency, environmental pollution, depletion of fossil fuel resources, and are now 12
replaced with comparatively more efficient, economical and cost-effective plants [5]. Fossil fuel 13
plants are posing threats to increased depletion in resources of fossil fuels along with 14
environmental deprivation. Many researchers in the world have done an investigation and have 15
reached the conclusion that it is an intense need to shift the resources of power generation from 16
non-renewable resources to renewables [6–8]. 17
As the time is progressing, the aim is to shift the strategy towards the design of an 18
efficient, consistent, and economical energy conversion system for low-temperature heat source 19
utilization, which could not be utilized otherwise [9]. Up to 80% of the power generation 20
facilities are utilizing fossil fuels (gasoline, natural gas, coal), and the remaining 20% of them are 21
utilizing renewable assets (such as geothermal energy, nuclear power, dams, wind power, 22
3
biomass, solar energy) [10]. For a country`s growth, sustainable development has become vital 1
and plays a decisive role. Sustainable development is well-defined as the social development 2
which is required in order to meet the present generations need without putting a risk at the needs 3
of future generations [11–13]. Sustainable development demands that an industry, which is 4
mainly based on non-renewable resources needs to be transformed into one based on renewable 5
resources [14]. 1st and 2
nd laws of thermodynamics can be effectively used for energy and exergy 6
analysis, which provide information regarding heat losses & processes irreversibility [15]. 7
Exergy analysis is a useful tool for the representation of variance among energy damages 8
and internal irreversibility in the processes [16]. 1st law of thermodynamics is usually used for 9
calculations of energy efficiency. However, the 1st law of thermodynamics is not enough to carry 10
out the optimization of steam power cycles. Coupling of 1st law with the 2nd
law of 11
thermodynamics is required and is a useful tool regarding power system analysis in terms of 12
energy and exergy. Exergy outlet can be defined as the system`s maximum useful output work. 13
Exergy destruction/lost work can be defined as the sum of each component`s lost work in a 14
power plant. Lost work can be estimated by tracking each individual equipment lost work and 15
summing all these [17,18]. During power plant operation, a part of the energy is rejected to the 16
environment i.e., in surface condenser operation, saturated steam is condensed by heat exchange 17
with cooling water pumping from the cooling tower, cooling water temperature is lowered by 18
heat exchange with air, but the heat carried away with the air is not recovered and rejected to the 19
environment. This type of energy is called Anergy [19]. 20
Rankine cycle and combined cycle energy and exergy analysis were studied by Kaushik 21
et al. [20] concluded that although condenser is the largest source for energy losses, boiler offers 22
4
maximum exergy loss especially in the combustion processes, can happen due to incomplete 1
combustion phenomena & insufficient insulation. The boiler of the steam power plant was 2
analyzed on basis of energy and exergy by Khani et al. [21], concluded that exergy efficiency is 3
increased to 0.19% & 0.37% respectively as excess air fraction is decreased to 0.4 and 0.15. 4
Furthermore, with the decrease in temperature of flue gases leaving the stack, from 137 °C to 5
90 °C, the increase in exergy efficiency was about 1.5%. Hamedan Steam power plant exergy 6
study was done by Ameri et al. [22]. The analysis included the effect on total efficiency due to 7
changes in environmental temperatures and unit loads. The authors concluded that % plant 8
efficiency is increased if the air is preheated before sending into the boiler. 9
Equipment in HRSG of combined cycle power plants were analyzed based on energy and 10
exergy analysis by Kaviri et al. [23]. Parameters investigated in the research comprised of the 11
pressure of steam drum, and heat exchanger arrangements in HRSG for high and low-pressure 12
parts. Combined cycle energetic, and exergy analyses were done by Ganjehkaviri et al. [24]. This 13
combined cycle is associated with HRSG. For different components of the cycle, energetic, 14
exergy and economic balances were applied. Based on the steam turbine exhaust, optimization 15
was done for the plant. Energetic and exergy efficiencies were calculated as a function of the 16
outlet vapor quality. The analysis showed that the optimized conditions of the system were 17
achieved for the outlet vapor quality of 88%, consequently, decreasing the total operational cost 18
of the cycle. Taillon and Blanchard [25] suggested new graphs for the determination of the 19
exergy efficiency of thermal power plants. These graphs were helpful to determine the efficiency 20
ranks as compared to the usually attained values for the industrial systems. Memon et al. [26] 21
used three approaches/parameters for the thermodynamic study of a combined cycle power plant: 22
5
exergo-economic, exergo-environmental, and statistics. Energy, exergy, and economic balances 1
were applied to the complete system. The effect of operational conditions on the efficiencies 2
(energy, exergy), power generation, and emissions was examined to obtain the optimized 3
operational conditions of the plant. For the development of exergo-economic analysis, objective 4
function is taken as the extension of exergy efficiency and minimization of total operating cost. 5
The present research aims to evaluate the efficiency of an operational power plant based 6
on energy and exergy analyses. The model of the power plant is prepared, modeled, and 7
simulated in Aspen HYSYS® V10. Exergy efficiency (%) and exergy destruction rate (kW) of 8
individual equipment in the power plant are computed. Case studies are included in this study to 9
analyze the effect of various operational parameters on the % efficiency of the various equipment. 10
11
2. Model Development 12
The power plant, under consideration, is operating on the principles of the Rankine and is 13
installed in Pakistan. The model of the steam power plant is prepared/modeled and simulated in 14
Aspen HYSYS® V10. 15
Fig. 1 represents the operational hierarchy of the power plant. The power plant consists of 16
a rice processing facility for which a powerhouse section is installed in the plant premise for the 17
electricity generation. 18
Underground raw water is pumped to the water storage tank using deep-well turbines. 19
Water is pumped to the reverse osmosis plant (R.O.) for the removal of total dissolved and 20
suspended solids. R.O. water is then pumped to the mixed bed polisher (MBP) unit for the 21
preparation of demineralized water. Water at the outlet of MBP unit is suitable to be utilized as 22
6
boiler feed water, as it contains very small fractions of solids, iron, and silica (in acceptable 1
limits). However, dissolved oxygen (DO) cannot be removed from these sections. Therefore, 2
water is the sent to de-aerator tank, where the DO removal takes place by counter-current contact 3
with saturated steam (coming from low-pressure header). This saturated steam is supplied to the 4
deaerator at 7 bar and 210 °C. Water at the outlet of deaerator is termed as “boiler feed water 5
(BFW)”, which is heated in the economizer (by heat exchange with flue gases coming from the 6
furnace), and then to steam drum. The flue gases are produced in the combustion chamber due to 7
the combustion of rice-husk as a fuel. 8
For the combustion process, both primary and secondary air are utilized, which are fed to 9
the combustion chamber using two forced draft fans. The flue gases exchange heat in the 10
following sequence: with the steam in two superheaters to produce superheated steam, water in 11
the steam drum to produce saturated steam, boiler feedwater in the two economizers, and with 12
the air in the air preheater. Since, ash is produced in this process, and flue gas may be carrying 13
some ash with it, therefore, the scrubber is installed (at the downstream of the air preheater) to 14
remove the ash contents from the flue gases by water spraying, and then is then vented at 15
ambient conditions. Secondary air is preheated in the air-preheater and sent to the furnace. 16
Water enters the steam drum at 210 – 220°C and saturated steam is produced from the 17
steam drum, which is converted to superheated steam in the superheaters. The superheated steam 18
is divided into two streams/fractions; one of the fraction is sent to the low-pressure header, where 19
saturated steam is produced, part of which is sent to the deaerator, while remaining part is sent to 20
the rice processing facility, while second fraction is sent to the turbine, where superheated steam 21
does work in the steam turbine, and the electricity is produced. The saturated steam leaves the 22
7
turbine, which is condensed in the water-cooled condenser, and recycled to the deaerator tank. 1
Cooling water (from the cooling tower) is used to condense the saturated steam in the condenser. 2
The operational conditions of the steam power plant are presented in Table 1. 3
4
3. Analysis of The Equipment 5
For in-depth analysis of the steam power plant, following parameters are fixed: 6
Steady state 7
Kinetic and potential exergies are neglected. 8
Reference conditions (Po = 1 bar and To = 25 °C). 9
The adiabatic system is considered for calculation purposes. 10
The thermodynamic property package selected for the system is “Peng-Robinson”. 11
Thermodynamics parameters (enthalpy, and entropy) are calculated using Aspen HYSYS® V10 12
and are used in the detailed calculations of the steam power plant. 13
14
3.1. Boiler 15
The fuel used in the process is rice-husk. The chemical exergy of the fuel is released during the 16
combustion in the boiler, which is transferred to the water. The power plant makes use of two 17
types of rice husk, having a difference in calorific values, namely, new rice husk having a 18
calorific value of 14,500 kJ/kg, and old rice husk having a calorific value of 13,700 kJ/kg. 19
However, the analysis is carried out based on new rice husk as a fuel. To perform exergy 20
analysis, the exergy flows are calculated for each stream, with specific enthalpy and entropy 21
8
values calculated at reference conditions. For a boiler, exergy destruction (𝐸𝑑) and % efficiency 1
(𝜀) are calculated as follows: 2
(Ed) = (mfΨf) + (msaΨsa) + (mpaΨpa) − (maΨa) − (mfgΨfg) − (msΨs) (1) 3
Exergy efficiency (%ε) = (ma Ψa)+ (mfg Ψfg)+ (ms Ψs)
(mf Ψf) + (msa Ψa) + (mpa Ψpa) × 100 (2) 4
5
3.1.1. Fuel exergy 6
The fuel used in the boiler is rice husk. For the calculation of fuel chemical exergy, its 7
composition is required which is presented in Table S1. 8
Rosen [21] has quantified an equation that is helpful in calculating the chemical exergy of 9
rice husk. Overall exergy of fuel can be calculated given the individual component`s standard 10
chemical exergy and molar ratio. 11
Ψf = Nf × Ψch,f (3) 12
where, 13
Nf = Mole fraction of each component in fuel 14
Ψch,f = Standard chemical exergy of each component in fuel 15
The chemical exergy values of individual components are presented in Table 2. 16
17
3.1.2. Flue gases leaving from boiler 18
Flue gases (produced in the combustion chamber of the boiler) leaves the furnace at a 19
temperature of 805.15 K. Since the gases are at high temperature, the temperature is reduced by 20
heat exchange with boiler feed water which increases its temperature from 373.75 K to 493.15 K, 21
while flue gases temperature reduces to 429.15 K. The flue gases come in countercurrent direct 22
9
contact with raw water which removes the fly ash from the flue gas and flue gases leave the stack 1
at a temperature of 313.15 K. For the demonstration of the chemical exergy of the combustion 2
products, the equation was stated by Ahmadi and Toghraie [27], presented as follows: 3
Ψg = Ʃxiech,i + RTo + Ʃxi lnxi (4) 4
Where, 5
ech,i = Individual component molar chemical exergy 6
xi = Individual component mole fraction of combustion product 7
8
3.1.3. Air entering the boiler 9
Primary and secondary airs are supplied to the combustion chamber by using forced draft fans. 10
Secondary air is mainly used to spread the rice husk in the combustion chamber. Primary air is 11
pre-heated to a temperature of 435.15 K and then fed to the combustion chamber. The 12
composition of the air used in the process is presented in Table S2. 13
14
3.2. Turbine 15
The steam turbine is installed at the site to meet the electricity demands of the plant. The steam 16
turbine can produce 2.97 MW (2970 kW) electricity. Superheated steam produced from the 17
boiler at a temperature and pressure of 673.15 K and 50.5 bar respectively, enters the turbine, 18
and its energy is utilized to produce work. The saturated steam leaves the steam turbine which is 19
condensed in a condenser. The balances of the turbine are applied as follows: 20
Mass Balance: m1 = m2 (5)21
Energy Balance: m1 h1 = m2 h2 (6) 22
10
Exergy Balance: 1
Exergy in (Ein) = E1 (7) 2
Exergy out (Eout) = E2 (8) 3
Exergy Efficiency (%𝜀) = (𝑊𝑡𝑢𝑟𝑏𝑖𝑛𝑒)
(𝐸1 − 𝐸2)⁄ × 100 (9) 4
Exergy Destruction (Ed) = E1 - E2 – Wturbine (10) 5
6
3.3. Condenser 7
Saturated steam leaving the turbine is condensed in the condenser by heat exchange with cooling 8
water pumping from the cooling tower. By means of heat exchange, saturated steam condensed 9
in the condenser, and is pumped to the deaerator. Cooling water is pumped back to the cooling 10
tower where its temperature is reduced by the exchange of heat with ambient air. The balances 11
on condenser are applied as follows: 12
Mass Balance: m2 + m3 = m4 + m5 (11) 13
Energy Balance: m2 h2 + m3 h3 = m4 h4 + m5 h5 (12) 14
Exergy Balance: 15
Exergy in (Ein) = E2 + E3 (13) 16
Exergy out (Eout) = E4 + E5 (14) 17
Exergy Efficiency (%𝜀) = (𝐸4 + 𝐸5)
(𝐸2 + 𝐸3)⁄ × 100 (15) 18
Exergy Destruction (Ed) = E2 + E3 – E4 – E5 (16) 19
20
3.4. Pump 21
11
Seven pumps are installed in the steam power plant; two pumps (1 working + 1 standby) to pump 1
condensate from water-cooled condenser to de-aerator, two pumps (1 working + 1 standby) to 2
pump boiler feed water from deaerator to the economizer, three pumps (1 working + 2 standby) 3
to pump raw water from raw water storage tank to the scrubber. 4
Win or Wpump values are taken on the operating condition to calculate % exergy efficiency. 5
The exergy efficiency (%) formula for all pumps in the power plant is the same. 6
Mass Balance: m6 = m7 (17) 7
Energy Balance: m6 h6 = m7 h7 (18) 8
Exergy Balance: 9
Exergy in (Ein) = E6 (19) 10
Exergy Out (Eout) = E7 (20) 11
Exergy Efficiency (%𝜀) = (𝐸7 − 𝐸6)
(𝑊𝑝𝑢𝑚𝑝)⁄ × 100 (21) 12
Exergy Destruction (Ed) = E6 – E7 + Wpump (22) 13
14
3.5. Deaerator 15
Deaerator provides boiler feed water by allowing counter-current contact of water and steam, 16
thus removing dissolved oxygen. Condensate from the water-cooled condenser and condensate 17
from production (rice-processing facility) come in counter-current contact with steam, generated 18
from the boiler. For the calculation purpose, the steam out through the deaerator is neglected. 19
Mass Balance: m8 + m9 + m10 = m11 (23) 20
Energy Balance: m8 h8 + m9 h9 + m10 h10 = m11 h11 (24) 21
12
Exergy Balance: 1
Exergy in (Ein) = E8 + E9 + E10 (25) 2
Exergy Out (Eout) = E11 (26) 3
Exergy Efficiency (%𝜀) = 𝐸11
(𝐸8 + 𝐸9 + 𝐸10)⁄ × 100 (27) 4
Exergy Destruction (Ed)= E8 + E9 + E10 – E11 (28) 5
6
4. Results 7
Mass exergy values of the process stream are calculated using Aspen HYSYS® V10. Table 3 8
represents the detailed exergy analysis of the process. Various components i.e., primary forced 9
draft fan, secondary forced draft fan, induced draft fan, boiler stop valve, etc. are neglected in 10
this analysis due to negligible contribution towards % exergy destruction rate. Based on this 11
energy analysis, the thermal efficiency of the boiler found to be 55.00 %. Based on exergy 12
analysis, the exergy efficiency of the boiler is 55.90 %, with the overall plant exergy efficiency 13
as 57.10 % 14
The % contribution to overall exergy destruction rate by each equipment is presented in 15
Fig. 2. The analysis shows that boiler is the major source of exergy destruction i.e., 93.99 %. The 16
higher value of exergy destruction is caused due to various reasons i.e., incomplete combustion 17
of rice husk in the furnace, poor ratio of fuel (rice husk) to air, and inappropriate insulations 18
across heating parts. Rice husk combustion in a boiler for conversion into thermal energy by 19
chemical energy, results in exergy consumption. This heat is transmitted to working fluid across 20
larger difference of temperature. In a boiler, various heat exchange equipment i.e., primary, and 21
13
secondary superheaters, economizers 1 & 2, air preheater are arranged in such a way to get 1
maximum heat transfer from flue gas to preheat the incoming boiler feed water to steam drum to 2
decrease fuel and air consumption. 3
Thermal/Polytropic efficiency calculated for the steam turbine is 60.12 %, while exergy 4
efficiency is 66.50 %. Two cooling water pumps are used for the flow of cooling water into the 5
condenser. Cooling tower system is installed at a considerable distance from other utility section. 6
This has led to an increase in the cooling tower power requirements as two pumps are required 7
for the supply of the adequate cooling water flow. This parameter has increased the power 8
requirements, and subsequently the utility costs. If this is replaced with a single cooling water 9
pump with a high flow rate pump, which will not only decrease in cost but will increase the % 10
exergy efficiency of the plant. 11
Various case studies are carried out on Aspen HYSYS® V10 to analyze the effect of 12
operational parameters on the performance of the system, which are presented as follows: 13
14
4.1. Case Study-1 15
Fig. 3 represents the effect of primary air temperature on the combustion. The analysis shows 16
that there is nearly a linear relationship between primary air temperature and flue gas production 17
rate. Primary air, before entering the boiler, is passed through the air preheater where it takes 18
heat from the flue gases coming from economizer 1. As the temperature of the primary air is 19
increased, the production rate of flue gases increases showing that the increase in temperature 20
has contributed towards an increase in the combustion efficiency. The comparatively reduced 21
amount of carbon is un-combusted, decrease in ash/residue production rate which helps in 22
14
improved % exergy efficiency of the boiler. This case-study is also in agreement with the 1
research conducted by various researchers [20, 27–30]. 2
3
4.2. Case Study-2 4
Fig. 4 represents the effect of properties of superheated steam temperature (at the turbine inlet) 5
on the polytropic efficiency of the turbine. The analysis shows that with the increase in steam 6
temperature from 350 to 450 °C, a 3% increase in polytropic efficiency is observed. Increase in 7
temperature of the system results in the increase in the superheating degree, which leads to the 8
improved operational efficiency of the steam turbine. This case-study is also in agreement with 9
the research conducted by various researchers [27, 29, 30]. 10
11
4.3. Case Study-3 12
Fig. 5 represents the effect of superheated steam temperature and pressure on the steam 13
requirements by the steam turbine, keeping electricity production capacity same i.e., 2.97 MW. 14
The analysis shows that with the increase in temperature and pressure of the superheated steam 15
(from the boiler), the steam flowrate requirement is decreased. This case-study is also in 16
agreement with the research conducted by various researchers [27, 29, 30]. 17
18
5. Conclusions 19
The objective of the work was to evaluate the performance of the steam power plant based on 20
energy and exergy analyses. The exergy analysis shows that the boiler is the major source of 21
exergy destruction rate in the process, mainly due to incomplete combustion, air to fuel ratio, 22
15
inappropriate insulations. It is recommended to install the variable flowmeters on the air stream 1
and apply an interlock control scheme with incoming feed for maintaining effective fuel to air 2
ratio. Insulation across the furnace and heating parts needs to be improved as it is another factor 3
towards the increase in the exergy destruction rate through the boiler. The exergy destruction rate 4
associated with the steam turbine is 3.81%, because the turbine is operating below the design 5
specifications i.e., 61 bar is the design pressure, while the steam turbine is operating at 50 bar, 6
which is causing decrease in thermal and exergy efficiency. Operating cooling tower with a 7
single pump can result in improved exergy efficiency of the plant. It will result in improved 8
exergy efficiency of the overall plant, eventually resulting in an improved cost of the plant. 9
10
Acknowledgments 11
The authors are thankful to the Department of Chemical Engineering, COMSATS University 12
Islamabad, Lahore Campus, for providing licensed version of Aspen HYSYS® V10. The 13
financial support from the University of Seoul and National Research Foundation under the 14
under the project (NRF- 2020R1I1A1A01072793) is gratefully acknowledged to conduct this 15
research. 16
17
Author Contributions 18
M.H.H. (Lecturer, Ph.D) and I.S. (Ph.D) wrote the manuscript and conducted the simulation 19
study. A.A. (Research Professor) performed the data analysis. M.H. (Professor) and Y.-K.P. 20
(Professor) planned the study and revised the manuscript. 21
22
16
Nomenclature 1
BFW Boiler feed water 2
Ed Exergy destruction (kW) 3
MBP Mixed bed polisher 4
Po Reference pressure (Bar) 5
R Ideal gas constant 6
R.O. Reverse osmosis 7
W Work produced (turbine) or work consumed (pump) 8
To Reference temperature (°C) 9
Greek Letters 10
ε Exergy efficiency (%) 11
𝑥𝑖 Mole fraction of component, i 12
𝑒𝑐ℎ,𝑖 Individual component molar exergy value 13
Subscripts 14
1 Steam at the inlet of turbine 15
2 Steam at the outlet of turbine 16
3 Cooling water at the inlet of condenser 17
4 Cooling water at the outlet of condenser 18
5 Condensate at the outlet of condenser 19
6 Stream at the pump inlet 20
7 Stream at the pump outlet 21
8 Polished water from the mixed bed polisher 22
17
9 Saturated steam from the low-pressure header 1
10 Recovered condensate from paddy section 2
11 Boiler feed water inlet to the boiler 3
4
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Table 1. Operational Conditions of The Steam Power Plant 1
Operating Parameters Value Unit
Flow Rate of Fuel 5,000 kg/h
Flow Rate of Secondary Air 69 m3/h
Flow Rate of Primary Air 134 m3/h
Temperature of Boiler Feed Water 101.0 °C
Pressure of Boiler Feed Water 51.0 Bar
Flow Rate of Steam Produced from Boiler 20,000 kg/h
Temperature of Steam Produced from Boiler 400.0 °C
Pressure of Steam Produced from Boiler 50.0 Bar
Steam Flow Rate to Turbine 15,000 kg/h
Steam Flow Rate to Production + Deaerator 5,000 kg/h
Power produced 2,970 kW
Temperature of Steam supplied to Production + Deaerator 210.0 °C
Pressure of Steam supplied to Production + Deaerator 7.0 Bar
Temperature of saturated steam from turbine 45.0 °C
Pressure of saturated steam from turbine 0.1 Bar
Condensate temperature from steam condenser to storage tank 45.0 °C
Condensate pressure from steam condenser to storage tank 10.0 Bar
Cooling Water Temperature at inlet of Condenser 32.0 °C
Cooling Water Pressure at inlet of Condenser 2.0 Bar
Cooling Water Temperature at outlet of Condenser 35.9 °C
Cooling Water Pressure at outlet of Condenser 1.9 Bar
2
Table 2. Chemical Exergy vValues of Rice-Husk Components 3
Component of Rice husk Chemical Exergy (kJ/mol)
Carbon (C) 410.26
Hydrogen (H2) 236.10
Sulfur (S) 609.60
Water (H2O) 9.49
Ash 8.20
22
Oxygen (O2) 3.97
Nitrogen (N2) 0.72
1
Table 3. Exergy Efficiency (%) and Exergy Destruction Rate Calculation of sSteam Power Plant 2
Equipment Exergy Efficiency, ε
(%)
Exergy Destruction, Ed
(MW)
% age
contribution
Boiler 55.80 36.90 93.99
Turbine 66.50 1.50 3.82
Surface Condenser 62.60 0.34 0.87
Raw Water Pump 52.80 0.00 0.00
Cooling Water Pump 56.90 0.30 0.76
Boiler Feed Water
Pump 55.70 0.03 0.08
Condensate Pump 55.50 0.00 0.00
De-aerator 51.30 0.19 0.48
Overall Plant 57.10 39.26 100
23
1
Fig. 1. Schematic diagram of the steam power plant. 2
3
Fig. 2. Power plant equipment contribution towards total exergy loss of the system. 4
24
1
Fig. 3. Effect of primary air temperature on production of flue gases and ash in the boiler. 2
3
4
Fig. 4. Influence of superheated steam parameters on steam flow rate. 5
6
25
1
Fig. 5. Effect of superheated steam properties on steam turbine operating efficiency. 2
3
